Local gas hold-up measurement in stirred fermenters. II. Fermenter gas hold-up characterization by a second order empirical model

Summary A second order polynomial, fitted by means of a Box-Hunter design, was used to describe the local gas hold-up of a stirred fermenter as a function of the stirrer speed, the aeration and the height of the point of measurement. Stirrer speed was found to be the main influential variable, whereas the aeration and the height of the point of measurement exert similar effects on local hold-up. Also interactions, mainly between the stirrer speed and the other two variables, were detected.     

Production of human hematopoietic progenitors in a clinical-scale stirred suspension bioreactor

Ex vivo expanded primitive hematopoietic cells can be utilized in bone marrow transplantation therapies to treat patients suffering from various cancers and hematopoietic malignancies. A high initial cell density (10⁶ cells/mL) and the supplement of soluble factors secreted by stromal feeders in combination with growth-promoting (interleukin-3 and stem cell factor) and growth-inhibiting (macrophage-inflammatory protein-1) cytokines resulted in high, long-term expansions (17-fold over a 14-day culture period) of human hematopoietic progenitors in a stirred suspension bioreactor. This study demonstrated that a transplantable dosage of human hematopoietic progenitor cells (8.1 ± 1.3 × 10⁶ colony forming unit-granulocyte/macrophage) can be generated from approximately 10 mL of bone marrow aspirate in a 14-day culture using a 250 mL suspension bioreactor system. © Rapid Science Ltd. 1998     

A cartridge oxygenator for mammalian cell culture in a stirred tank bioreactor

Summary Tubing made of membrane with high oxygen permeability is often used in supplying oxygen to animal cell culture bioreactors. We have fabricated the tubing into a cartridge configuration. Such an arrangement allows damaged tubing to be replaced conveniently and eases the maintenance of such an oxygenator in bioreactors.     

Determination of the average shear rate in a stirred and aerated tank bioreactor

A method for evaluating the average shear rate () in a stirred and aerated tank bioreactor has been proposed for non-Newtonian fluids. The volumetric oxygen transfer coefficient (k _L a) was chosen as the appropriate characteristic parameter to evaluate the average shear rate (). The correlations for the average shear rate as a function of N and rheological properties of the fluid (K and n) were obtained for two airflow rate conditions (ϕ_air). The shear rate values estimated by the proposed methodology lay within the range of the values calculated by classical correlations. The proposed correlations were utilized to predict the during the Streptomyces clavuligerus cultivations carried out at 0.5 vvm and four different rotational impeller speeds. The results show that the values of the average shear rate () varied from 437 to 2,693 s⁻¹ by increasing with N and flow index (n) and decreasing with the fluid consistency index (K).     

In situ filtration of Anchusa officinalis culture in a cell-retention stirred tank bioreactor

Summary The effect of agitation and aeration on filtration of Anchusa officinalis culture in a stirred tank bioreactor integrated with an internal filter unit was investigated. Increases in suction head of the pump that drove the filtration process were measured at impeller speeds of 100 and 200 rpm. Surprisingly, suction head attained at 200 rpm was about 40% higher than at 100 rpm. Direct observation of the cake deposition process in the reactor using a dilute cell suspension revealed that the filter cake formed at 100 rpm was thicker, but less compact. Aeration at 0.4 vvm was shown to have little effect on the filtration rate, since the bulk fluid flow was dominated by the impeller hydrodynamics. The initial flux can be recovered by filter backwashing with compressed air at a flow rate of 0.6 vvm for a duration of 5 minutes.     

Ethanol production by immobilized whole cells ofZymomonas mobilis in a continuous flow expanded bed bioreactor and a continuous flow stirred tank bioreactor

Continuous ethanol fermentation by immobilized whole cells ofZymomonas mobilis was investigated in an expanded bed bioreactor and in a continuous stirred tank reactor at glucose concentrations of 100, 150 and 200 g L^–1. The effect of different dilution rates on ethanol production by immobilized whole cells ofZymomonas mobilis was studied in both reactors. The maximum ethanol productivity attained was 21 g L^–1 h^–1 at a dilution rate of 0.36 h^–1 with 150 g glucose L^–1 in the continuous expanded bed bioreactor. The conversion of glucose to ethanol was independent of the glucose concentration in both reactors.     

An approximate solution for a transient two-phase stirred tank bioreactor with nonlinear kinetics

The derivation of an approximate solution method for models of a continuous stirred tank bioreactor where the reaction takes place in pellets suspended in a well-mixed fluid is presented. It is assumed that the reaction follows a Michaelis-Menten-type kinetics. Analytic solution of the differential equations is obtained by expanding the reaction rate expression at pellet surface concentration using Taylor series. The concept of a pellet's dead zone is incorporated; improving the predictions and avoiding negative values of the reagent concentration. The results include the concentration expressions obtained for (a) the steady state, (b) the transient case, imposing the quasi-steady-state assumption for the pellet equation, and (c) the complete solution of the approximate transient problem. The convenience of the approximate method is assessed by comparison of the predictions with the ones obtained from the numerical solution of the original problem. The differences are in general quite acceptable.     

Fluid mixing and oxygen transfer in cell suspensions ofTaxus chinensis in a novel stirred bioreactor

In high-density plant cell cultures, mixing and mass transfer are two key issues, which should be emphasized for process optimization. In this work, both mixing and oxygen transfer characteristics of cell suspensions ofTaxus chinensis were studied in a new centrifugal impeller bioreactor with a working volume of 1.2 L. The mixing time (t _M) and the volumetric oxygen transfer coefficient (K _L a) under different operational conditions were determined in both tap water and cell suspensions of 100–400 g fresh weight/L (i.e., 5.65–23.1 g DW/L). At an aeration rate of 0.1 L/min,t _M decreased from 10.6s at 30 rpm to 2.89 s at 200 rpm under 100 g FW/L, and from 9.63 s (120 rpm) to 4.05 s (300 rpm) under 400 g FW/L. Compared with the effect of agitation, aeration was less significant to the suspension mixing. At a relatively high agitation speed (e.g., 200 rpm),t _M remained almost the same even though aeration rate was changed from 0.1 to 0.4 L/min. Thet _M value increased slowly from 3.98 to 5.26 s at 120 rpm when the cell density was raised from 100 to 250 g FW/L. A rapid increase of botht _M and the suspension viscosity was observed at a cell density above 300 g FW/L. As expected, theK _L a value increased with an increase of aeration rate and agitation speed, but decreased with an increase of cell density. The quantitative data obtained here are useful to investigate the effect of mixing stress on the cell physiology and metabolism ofTaxus chinensis in the bioreactor. This paper is dedicated by JJZ to his colleague Prof. Jun-Tang Yu on the occasion of his 70 birthday.     

Ex vivo expansion of bone marrow mesenchymal stem cells using microcarrier beads in a stirred bioreactor

Bone marrow mesenchymal stem cells (bmMSCs) have recently gained attention as a useful resource in the fields of regenerative medicine and tissue engineering. However, the number of bmMSCs obtained from available donors is very low. Here we developed a culture strategy for in vitro expansion of bmMSCs in a 1.5 L stirred bioreactor with microcarrier beads. First, the microcarriers (Cytodex 3) were equilibrated in culture medium containing 3% fetal bovine serum (FBS) for at least 30 min prior to cell addition. After inoculation, the FBS concentration of the medium was maintained at 3% (v/v) in the first 24 h and thereafter maintained at 1% (v/v) and a developed feeding regimen was applied over 5 days. The maximum cell density of 2.6 × 10⁶ cells/mL was achieved at day 5, corresponding to a 10.4 ± 0.8 fold increases in total cell number. Among the harvested cells, 98.95% expressed CD29 and 84.48% expressed CD90, suggesting that the majority of expanded bmMSCs still retained their differentiation potential. Therefore, the developed microcarrier-based stirred bioreactor culture system is an effective method to generate significant numbers of bmMSCs for potential applications and research studies.     

Scale-up of biotransformation process in stirred tank reactor using dual impeller bioreactor

The gas-liquid mass transfer coefficient K(L)a in the fermenter is a strong function of mode of energy dissipation and physico-chemical properties of the liquid media. A combination of disc turbine (DT) and pitched blade turbine down flow (PTD) impellers has been tested in laboratory bioreactor for gas hold-up and gas-liquid mass transfer performance for the growth and biotransformation medium for an yeast isolate VS1 capable of biotransforming benzaldehyde to L-phenyl acetyl carbinol (L-PAC) and compared with those in water.Correlations have been developed for the prediction of the fractional gas hold-up and gas-liquid mass transfer coefficient for the above media. The mass transfer coefficient and respiration rate have been determined in the shake flask for the growth as well as for biotransformation medium. These results, then have been used to optimize the operating parameters (impeller speed and aeration) for growth and biotransformation in a laboratory bioreactor. The comparison of cell mass production and L-PAC production in the bioreactor has been done with that obtained in shake flask studies.     

Hydrodynamic performance of a single-use aerated stirred bioreactor in animal cell culture: applications of tomography,dynamic gas disengagement (DGD), and CFD

Bioprocess and Biosystems Engineering - The hydrodynamics of gas–liquid two-phase flow in a single-use bioreactor were investigated in detail both experimentally and numerically. Electrical...     

Characteristics of a mesoporous silicate immobilized trypsin bioreactor in organic media

Mesoporous silicates (MPS) materials are attractive materials for immobilizing proteins/enzymes because of their well ordered structures, large surface areas (up to 1000 m(2) g(-1)), narrow pore size distributions, large pore diameters, and pore volumes. MPS with average pore diameters ranging from 28 to 300 Angstroms were prepared using cationic and nonionic surfactants. The influence of water content, pH, storage, and thermal treatment on the activity of trypsin immobilized onto MPS was investigated. In a range of solvents, the amidolytic activity of immobilized trypsin was higher than that of the lyophilized preparation. Significant increases in k(cat)/K(M) occurred in propanol, ethanol, methanol, and formamide of 90, 62, 45 and 26, respectively. The observed increases were primarily a result of substantial increases in k(cat).     

Combined effect of hydrodynamic and interfacial flow parameters on lysozyme deactivation in a stirred tank bioreactor

The dynamic environment within a bioreactor and in the purification equipment is known to affect the activity and yield of enzyme production. The present research focuses on the effect of hydrodynamic flow parameters (average energy dissipation rate, maximum energy dissipation rate, average shear rate, and average normal stress) and the interfacial flow parameters (specific interfacial area and mass transfer coefficient) on the activity of lysozyme. Flow parameters were estimated using CFD simulation based on the k-epsilon approach. Enzyme deactivation was investigated in 0.1, 0.3, 0.57, and 1 m i.d. vessels. Enzyme solution was subjected to hydrodynamic stress using various types of impellers and impeller combinations over a wide range of power consumption (0.03 < P(G)/V < 7, kW/m3). The effects of tank diameter, impeller diameter, blade width, blade angle, and the number of blades on the extent of deactivation were investigated. At equal value of P(G)/V, epsilon(max), and gamma(avg), the extent of deactivation was dramatically different for different impeller types. The extent of deactivation was found to correlate well with the average turbulent normal stress and the mass transfer coefficient.     

Microbial dynamics in a continuous stirred tank bioreactor exposed to an alternating sequence of organic compounds

Microbial dynamics during aerobic biodegradation of an alternating mixture of organic compounds was investigated experimentally in a continuous stirred tank bioreactor (CSTB). A mathematical model describing this system was developed and tested using the experimental results. A model microbial culture consisting of Pseudomonas sp. JS150, a monochlorobenzene (MCB) degrader, and Xanthobacter autotrophicus GJ10, a 1,2-dichloroethane (DCE) degrader, each with exclusive degradation capabilities, was used. The CSTB was inoculated with both microbial strains and exposed to an alternating sequence of the two compounds at noninhibitory concentrations. Concentrations of each microbial strain, of each organic compound, and of degradation product evolved, as well as specific microbial activities via oxygen uptake tests, were monitored. Reduction of the residual DCE discharged from the bioreactor after an MCB to DCE transition was successfully achieved by continuously feeding a low flow of a concentrated solution of both compounds.     

Studies on the production of enantioselective nitrilase in a stirred tank bioreactor by Pseudomonas putida MTCC 5110

Nitrilases constitute an important class of hydrolases, having numerous industrial applications. The present work aims to address the production of nitrile hydrolyzing enzymes from Pseudomonas putida MTCC 5110 in a 6l bioreactor. Effect of various physico-chemical conditions and process parameters like pH, temperature, aeration and agitation rates and inducer concentration was studied. Further, the enzyme activity was enhanced by adopting the inducer feeding strategy. Various biochemical engineering parameters pertaining to the cultivation of P. putida in different physico-chemical conditions were reported. Finally, segregation of growth phase from the enzyme production phase allowed significant reduction in total fermentation time.